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EP0114477A1 - Procédé et dispositif pour éliminer des oxides de soufre de gaz de fumée chauds - Google Patents

Procédé et dispositif pour éliminer des oxides de soufre de gaz de fumée chauds Download PDF

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Publication number
EP0114477A1
EP0114477A1 EP83307556A EP83307556A EP0114477A1 EP 0114477 A1 EP0114477 A1 EP 0114477A1 EP 83307556 A EP83307556 A EP 83307556A EP 83307556 A EP83307556 A EP 83307556A EP 0114477 A1 EP0114477 A1 EP 0114477A1
Authority
EP
European Patent Office
Prior art keywords
reaction zone
absorption agent
powder
flue gases
hot flue
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Granted
Application number
EP83307556A
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German (de)
English (en)
Other versions
EP0114477B2 (fr
EP0114477B1 (fr
Inventor
Vinay K. Bhatia
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
FLSmidth and Co AS
Original Assignee
FLSmidth and Co AS
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
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First worldwide family litigation filed litigation Critical https://patents.darts-ip.com/?family=8144337&utm_source=google_patent&utm_medium=platform_link&utm_campaign=public_patent_search&patent=EP0114477(A1) "Global patent litigation dataset” by Darts-ip is licensed under a Creative Commons Attribution 4.0 International License.
Application filed by FLSmidth and Co AS filed Critical FLSmidth and Co AS
Priority to AT83307556T priority Critical patent/ATE26545T1/de
Publication of EP0114477A1 publication Critical patent/EP0114477A1/fr
Application granted granted Critical
Publication of EP0114477B1 publication Critical patent/EP0114477B1/fr
Publication of EP0114477B2 publication Critical patent/EP0114477B2/fr
Anticipated expiration legal-status Critical
Expired - Lifetime legal-status Critical Current

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    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/46—Removing components of defined structure
    • B01D53/48—Sulfur compounds
    • B01D53/50—Sulfur oxides
    • B01D53/501—Sulfur oxides by treating the gases with a solution or a suspension of an alkali or earth-alkali or ammonium compound

Definitions

  • the present invention relates to a method of and apparatus for removing sulfur oxides and other acidic gases from hot flue gases, in which an absorption agent and liquid water are introduced and dispersed in a stream of hot flue gases in a reaction zone wherein sulfur oxides and other acidic gases are absorbed by and reacted with the absorption agent in the presence of evaporating liquid water, producing a dry powder comprising reaction products and unreacted absorption agent suspended in flue gas, whereafter the powder is separated from the flue gas in a separating zone and partly recycled to the reaction zone.
  • Such a method will hereinafter be described as "of the kind described”.
  • the main advantages of the wet methods are: High sulfur oxide removal even at high sulfur oxide concentrations in the hot flue gas and high absorbent utilization.
  • the main disadvantages are: Undesirable end products occuring as a sludge and thus presenting serious disposal problems and water saturated exit gas which must be heated prior to discharge to the atmosphere. Furthermore, clogging and corrosion in the scrubber lead to operational difficulties and unavailability of wet scrubbers.
  • the semi-dry methods provide highly improved sulfur oxide removal and absorbent utilization compared to the dry methods, although in general not as high as that which may be obtained by the wet methods, easily dischargeable desulfurized flue gas and a dry, flowable solid powder as end product.
  • GB-A-2,021,086 describes a similar process utilizing a less expensive absorption agent: Ca(OH) 2 suspended in water. Improved lime utilization is achieved by avoiding fly ash removal from the hot inlet gas and by recirculation of a part of the powdery end product from the spray-dryer to the aqueous slurry directed to the spray-dryer. The viscosity of the aqueous slurry of absorption agent and recirculated powder, however, puts narrow limits to the amount of powder recirculated.
  • AST approximate to saturation temperature
  • This method provides an extremely intimate gas solid contact for several reasons:
  • the method of the invention allows a significantly higher concentration of suspended material in the reaction zone than that achieved by methods operating with a descending or horizontal co-current gas particle flow.
  • the temperature of the hot flue gases introduced into the reaction zone is in general above 120°C.
  • the temperature is in general within the range 110° to 250°, typically 140° to 180°C.
  • fly ash may be removed totally or partially from the hot flue gases before it is introduced into the reaction zone.
  • the velocity of the hot flue gases entering the reaction zone may vary depending on the load and size of the particles circulating in the reaction zone. However, it must be sufficiently high to maintain particle support in the reaction zone and prevent particle fall-out from the bottom of the zone.
  • the reduced velocity of the flue gases must be sufficiently high to ensure transport of the particles out of the upper part of the reaction zone, but sufficiently low to ensure proper material build-up in the reaction zone.
  • the velocity of the hot flue gases is reduced from between 10 and 60 m/sec., preferentially between 25 and 45 m/sec. to between 2 and 20 m/sec., preferentially between 3 and 6 m/sec., and the reduction in velocity corresponds to a velocity ratio v initial /v reduced within the range 3 to 20, preferably 4 to 9.
  • Such boundary layer separation is preferentially generated by directing the hot flue gases through a divergent annular frusto-conical bottom part of the reaction zone, in particular having an apex angle greater than 12°, preferably between 12° and 120°, in particular between 40° and 90°. Apex angles greater than 120° are not desirable because of the risk of undesirable material build-up on the frusto-conical bottom of the reaction zone.
  • the absorption agent is preferentially selected among members of the group comprising oxides and hydroxides of calcium and magnesium and oxides, hydroxides and carbonates of alkali metals.
  • Ca(OH) 2 preferentially prepared by slaking in a detention slaker, attrition slaker or ball mill, is the preferred absorption agent.
  • Absorption agent may be introduced as a dry powder or suspended or dissolved in water, and water may be introduced separately, mixed with the absorption agent, or only part of the water may be mixed with the absorption agent.
  • the absorption agent is preferentially introduced suspended or dissolved in water.
  • the water or the suspension or solution of absorption agent in water is preferentially introduced in the reaction zone at a position where the flue gas velocity is high.
  • the powder comprises reaction products and unreacted absorption agent.
  • the flue gas entering the reaction zone will in general entrain fly ash particles which will be precipitated in the separating zone.
  • Fly ash may contain reactive alkalies capable of reacting with sulfur oxides and other acidic gases under proper conditions, resulting in a reduced demand for absorption agent.
  • the powder recirculation rate is equal to 10 to 70 times, preferentially 15 to 30 times, the input rate of absorption agent and solid particles present in the hot flue gas, where the input rate of the absorption agent is defined as the input rate of fresh absorption agent not comprising unreacted absorption agent introduced with the powder.
  • the material retention time in the reaction zone is controlled by the powder recirculation rate.
  • the average particle diameter of the recirculated powder is preferentially within the range 20 to 250 micron. This preferred size may be ensured by subjecting the dry powder separated in the separating zone to size adjustment, e.g. screening, or size reduction by comminution, e.g. in a hammer mill, before it is recirculated to the reaction zone.
  • size adjustment e.g. screening
  • size reduction by comminution e.g. in a hammer mill
  • AST values are obtained when water is introduced into the reaction zone in an amount corresponding to 50 to 100% of the amount needed to cool the flue gas to the adiabatic saturation temperature.
  • AST falls in general in the range of 0 to 40°C, preferentially in the range 5 to 20°C, and in particular within the range 8 to l6 0 C.
  • the exit gas may be reheated, e.g. by by-passing a portion of the hot flue gas around the reaction zone.
  • the flue gas After leaving the reaction zone, the flue gas is dedusted, whereby powder comprising unreacted absorption agent, reaction products and fly ash are removed in the separating zone in one or two steps in separators known per se.
  • the separating zone comprises two sub-zones, a first sub-zone for precipitation of coarse particles and a second sub-zone for precipitation of fine particles.
  • the invention also includes apparatus for carrying out the method, which apparatus includes a reaction chamber having an upright axis, an annular bottom wall which slopes downwardly and inwardly, a central inlet for hot flue gas in the bottom wall, ducts for feeding absorption agent, powder and water into the lower part of the reaction chamber, and a suspension outlet at the top of the reaction chamber for connection to a particle precipitator having a powder outlet duct communicating with the powder feeding duct.
  • the reaction chamber is preferentially tubular.
  • the extremely intimate gas/solid contact and the high concentration of solid material in the reaction zone permit the use of a very compact apparatus of simple design and corresponding low investment costs.
  • the absorption agent is introduced into the reaction chamber suspended or dissolved in water, water and absorption agent being fed through the same feeding duct to the reaction chamber.
  • the feeding duct for the water or the water and absorption agent is preferentially provided with a gas liquid spray nozzle e.g. a venturi injection nozzle.
  • the particle precipitator comprises a coarse separator, e.g. a cyclone separator, arranged upstream of a fine separator, e.g. an electrostatic filter or a fabric filter.
  • a coarse separator e.g. a cyclone separator
  • a fine separator e.g. an electrostatic filter or a fabric filter.
  • the apparatus comprises a tubular reaction chamber 1 provided with an annular frusto-conical bottom wall 2 and an inlet duct 3 for hot flue gases, an inlet duct 4 for absorption agent suspended or dissolved in water, and an inlet duct 5 for recirculated dry powder.
  • the top of the reaction chamber is connected to a particle precipitator comprising a separating cyclone 6 with a material outlet 7 provided with a splitting gate 8 dividing the powder into two streams, one being recirculated to the reaction chamber 1, the other being discharged as waste product through a duct 9.
  • the exit gas from the separating cyclone 6 is directed via a gas outlet duct 10 to an electrostatic filter 6' with a material outlet 7' and a gas outlet duct 10'.
  • the fine powder precipitated in the electrostatic filter may be discharged as waste product or recirculated totally or partially to the reaction chamber.
  • the inlet duct 4 may be replaced by two ducts, one for water and another for absorption agent.

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  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • General Chemical & Material Sciences (AREA)
  • Environmental & Geological Engineering (AREA)
  • Biomedical Technology (AREA)
  • Analytical Chemistry (AREA)
  • Health & Medical Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Treating Waste Gases (AREA)
  • Manufacture And Refinement Of Metals (AREA)
  • Cyclones (AREA)
  • Photoreceptors In Electrophotography (AREA)
  • Transition And Organic Metals Composition Catalysts For Addition Polymerization (AREA)
  • Polyoxymethylene Polymers And Polymers With Carbon-To-Carbon Bonds (AREA)
EP83307556A 1982-12-22 1983-12-12 Procédé et dispositif pour éliminer des oxides de soufre de gaz de fumée chauds Expired - Lifetime EP0114477B2 (fr)

Priority Applications (1)

Application Number Priority Date Filing Date Title
AT83307556T ATE26545T1 (de) 1982-12-22 1983-12-12 Verfahren und vorrichtung zur entfernung von schwefeloxiden aus heissen abgasen.

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DK566682 1982-12-22
DK5666/82 1982-12-22

Publications (3)

Publication Number Publication Date
EP0114477A1 true EP0114477A1 (fr) 1984-08-01
EP0114477B1 EP0114477B1 (fr) 1987-04-15
EP0114477B2 EP0114477B2 (fr) 1991-04-10

Family

ID=8144337

Family Applications (1)

Application Number Title Priority Date Filing Date
EP83307556A Expired - Lifetime EP0114477B2 (fr) 1982-12-22 1983-12-12 Procédé et dispositif pour éliminer des oxides de soufre de gaz de fumée chauds

Country Status (10)

Country Link
US (1) US4555390A (fr)
EP (1) EP0114477B2 (fr)
JP (1) JPH0653209B2 (fr)
AT (1) ATE26545T1 (fr)
CA (1) CA1212220A (fr)
CS (1) CS252468B2 (fr)
DD (1) DD215573A5 (fr)
DE (1) DE3370942D1 (fr)
DK (1) DK154118C (fr)
PL (1) PL143667B1 (fr)

Cited By (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP0196481A1 (fr) * 1985-03-13 1986-10-08 Von Roll Ag Procédé et dispositif pour séparer des composés polluants d'un courant de gaz
US4891194A (en) * 1985-10-16 1990-01-02 L. & C. Steinmuller Gmbh Method for scrubbing flue gases from a firing unit
EP0370648A1 (fr) * 1988-11-22 1990-05-30 United Kingdom Atomic Energy Authority Séparation de composants gazeux
US5382418A (en) * 1992-03-03 1995-01-17 Metallgesellschaft Aktiengesellschaft Process for removing pollutants from combustion exhaust gases
US5723099A (en) * 1996-05-17 1998-03-03 Steinke; Richard A. Method and apparatus for remediation of toxic flue gases
WO1998039082A1 (fr) * 1997-03-06 1998-09-11 Metallgesellschaft Aktiengesellschaft Procede d'elimination des polluants contenus dans des gaz de combustion
WO2013075719A1 (fr) 2011-11-23 2013-05-30 Flsmidth A/S Procédé et équipement de fabrication de clinker de ciment
CN114226066A (zh) * 2021-12-20 2022-03-25 中国建筑材料科学研究总院有限公司 一种从尾气中回收再利用SiO2粉末的方法及装置

Families Citing this family (15)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
FI78401B (fi) * 1985-04-24 1989-04-28 Tampella Oy Ab Foerfarande och anordning foer att bringa roekgasernas gasformiga svavelfoereningar saosom svaveldioxid att reagera till fasta foereningar som separeras fraon roekgaserna.
US5100633A (en) * 1985-11-07 1992-03-31 Passamaquoddy Technology Limited Partnership Method for scrubbing pollutants from an exhaust gas stream
US5499587A (en) * 1986-06-17 1996-03-19 Intevep, S.A. Sulfur-sorbent promoter for use in a process for the in-situ production of a sorbent-oxide aerosol used for removing effluents from a gaseous combustion stream
CS206990A2 (en) * 1989-05-02 1991-09-15 Chiyoda Chem Eng Construct Co Method of waste gas cleaning that contains dust and chemical impurities and equipment for this method realization
FI84435C (fi) * 1990-02-23 1995-02-22 Ahlstroem Oy Foerfarande och anordning foer rengoering av foeroreningar innehaollande gaser
EP0637988A1 (fr) * 1991-08-22 1995-02-15 Foster Wheeler Energia Oy Procede de purification de gas de four
US5470556A (en) * 1993-12-22 1995-11-28 Shell Oil Company Method for reduction of sulfur trioxide in flue gases
US5997823A (en) * 1997-08-18 1999-12-07 Noxso Corporation Processes and apparatus for removing acid gases from flue gas
WO2006086251A2 (fr) * 2005-02-04 2006-08-17 Fuel Tech, Inc. Injection cible de reduction a so3
US8695516B2 (en) * 2009-04-21 2014-04-15 Industrial Accessories Company Pollution abatement process for fossil fuel-fired boilers
US20100263577A1 (en) * 2009-04-21 2010-10-21 Industrial Accessories Company Pollution abatement process for fossil fuel-fired boilers
US10155227B2 (en) 2012-08-24 2018-12-18 Mississippi Lime Company Systems and method for removal of acid gas in a circulating dry scrubber
US9751043B1 (en) 2014-09-05 2017-09-05 Mississippi Lime Company Systems and method for removal of acid gas in a circulating dry scrubber
US10668480B1 (en) 2014-09-05 2020-06-02 Mississippi Lime Company Systems and method for removal of acid gas in a circulating dry scrubber
US11365150B1 (en) 2018-07-18 2022-06-21 Mississippi Lime Company Lime hydrate with improved reactivity via additives

Citations (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3932587A (en) 1971-12-09 1976-01-13 Rockwell International Corporation Absorption of sulfur oxides from flue gas
DE2553675A1 (de) * 1975-04-07 1976-10-21 American Air Filter Co Verfahren und anordnung zum entfernen von so tief 2 aus schornsteingasen
US4150096A (en) * 1977-10-31 1979-04-17 Nelms William M Process for treating combustion gases
GB2021086A (en) 1978-05-19 1979-11-28 Niro Atomizer As Process for flue gas desulphurization
US4197278A (en) 1978-02-24 1980-04-08 Rockwell International Corporation Sequential removal of sulfur oxides from hot gases
DE2901637A1 (de) * 1979-01-17 1980-07-24 Steag Ag Verfahren zur entfernung von chlorund fluorverbindungen in rauchgasen, insbesondere zur verminderung der salzfracht von abwaessern einer industriellen rauchgasentschwefelung
DK395979A (da) 1979-09-21 1981-03-22 Anhydro As Fremgangsmaade til fra roeggasser at fraskille aggressive og miljeskadelige luftarter og anlaeg til udoevelse af fremgangsmaaden

Family Cites Families (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JPS499471A (fr) * 1972-05-24 1974-01-28
JPS498459A (fr) * 1972-05-24 1974-01-25
JPS5239382B2 (fr) * 1972-05-24 1977-10-05
JPS5239382A (en) * 1975-09-23 1977-03-26 Meidensha Electric Mfg Co Ltd Gate control semiconductor element
DE2739509C2 (de) * 1977-09-02 1982-09-16 Babcock-BSH AG vormals Büttner-Schilde-Haas AG, 4150 Krefeld Verfahren und Vorrichtung zur Reinigung eines Abgasstromes
US4293524A (en) * 1978-09-20 1981-10-06 Teller Environmental Systems, Inc. Method and apparatus for cooling and neutralizing acid gases

Patent Citations (9)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3932587A (en) 1971-12-09 1976-01-13 Rockwell International Corporation Absorption of sulfur oxides from flue gas
DE2553675A1 (de) * 1975-04-07 1976-10-21 American Air Filter Co Verfahren und anordnung zum entfernen von so tief 2 aus schornsteingasen
US4150096A (en) * 1977-10-31 1979-04-17 Nelms William M Process for treating combustion gases
US4197278A (en) 1978-02-24 1980-04-08 Rockwell International Corporation Sequential removal of sulfur oxides from hot gases
US4197278B1 (en) 1978-02-24 1996-04-02 Abb Flakt Inc Sequential removal of sulfur oxides from hot gases
GB2021086A (en) 1978-05-19 1979-11-28 Niro Atomizer As Process for flue gas desulphurization
DE2901637A1 (de) * 1979-01-17 1980-07-24 Steag Ag Verfahren zur entfernung von chlorund fluorverbindungen in rauchgasen, insbesondere zur verminderung der salzfracht von abwaessern einer industriellen rauchgasentschwefelung
DK395979A (da) 1979-09-21 1981-03-22 Anhydro As Fremgangsmaade til fra roeggasser at fraskille aggressive og miljeskadelige luftarter og anlaeg til udoevelse af fremgangsmaaden
DE3034896A1 (de) 1979-09-21 1981-04-09 Anhydro A/S, Søborg Verfahren zur abscheidung aggressiver und umweltschaedlicher gase aus abgasen, und anlage zur ausuebung des verfahrens

Non-Patent Citations (1)

* Cited by examiner, † Cited by third party
Title
"Rauchgasreinigung nach der Abfallverbrennung", 12TH WASTE ECONOMY SEMINAR, 1981, pages 242 - 259

Cited By (11)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP0196481A1 (fr) * 1985-03-13 1986-10-08 Von Roll Ag Procédé et dispositif pour séparer des composés polluants d'un courant de gaz
US4891194A (en) * 1985-10-16 1990-01-02 L. & C. Steinmuller Gmbh Method for scrubbing flue gases from a firing unit
EP0370648A1 (fr) * 1988-11-22 1990-05-30 United Kingdom Atomic Energy Authority Séparation de composants gazeux
US5382418A (en) * 1992-03-03 1995-01-17 Metallgesellschaft Aktiengesellschaft Process for removing pollutants from combustion exhaust gases
DE4206602C2 (de) * 1992-03-03 1995-10-26 Metallgesellschaft Ag Verfahren zum Entfernen von Schadstoffen aus Verbrennungsabgasen und Wirbelschichtreaktor hierzu
US5723099A (en) * 1996-05-17 1998-03-03 Steinke; Richard A. Method and apparatus for remediation of toxic flue gases
US5795549A (en) * 1996-05-17 1998-08-18 American Mobility Ltd. Appraratus for remediation of toxic flue gases
WO1998039082A1 (fr) * 1997-03-06 1998-09-11 Metallgesellschaft Aktiengesellschaft Procede d'elimination des polluants contenus dans des gaz de combustion
WO2013075719A1 (fr) 2011-11-23 2013-05-30 Flsmidth A/S Procédé et équipement de fabrication de clinker de ciment
CN114226066A (zh) * 2021-12-20 2022-03-25 中国建筑材料科学研究总院有限公司 一种从尾气中回收再利用SiO2粉末的方法及装置
CN114226066B (zh) * 2021-12-20 2024-04-12 中国建筑材料科学研究总院有限公司 一种从尾气中回收再利用SiO2粉末的方法及装置

Also Published As

Publication number Publication date
CA1212220A (fr) 1986-10-07
JPH0653209B2 (ja) 1994-07-20
CS980183A2 (en) 1987-02-12
CS252468B2 (en) 1987-09-17
EP0114477B2 (fr) 1991-04-10
DK588883A (da) 1984-06-23
EP0114477B1 (fr) 1987-04-15
ATE26545T1 (de) 1987-05-15
DK154118B (da) 1988-10-17
JPS59166229A (ja) 1984-09-19
DD215573A5 (de) 1984-11-14
PL143667B1 (en) 1988-03-31
DK588883D0 (da) 1983-12-21
DK154118C (da) 1989-03-20
US4555390A (en) 1985-11-26
DE3370942D1 (en) 1987-05-21
PL245276A1 (en) 1984-07-16

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